Process for the production of olefins

ABSTRACT

OLEFINS IN THE RANGE OF 6-20 CARBON ATOMS ARE PREPARED BY FEEDING LOWER OLEFIN (E.G., ETHYLENE), LOWER ALKYL ORGANOMETALLIC (E.G., TRIETHYL ALUMINUM) AND PRODUCT OLEFIN INTO A REACTION SYSTEM IN WHICH CHAIN BUILD UP OCCURS (E.G., CHAIN GROWTH OR CATALYTIC POLYMERIZATION). THE REACTION EFFLUENT IS FLASHED TO REMOVE PRODUCT OLEFIN AND LOWER BOILING OLEFIN. THE REMAINDER OF THE EFFLUENT CONTAINS HIGHER ALKYL ORGANOMETALLIC AND IS SUBJECTED TO AN ALKYL DISPLACEMENT REACTION USING LOWER OLEFIN (E.G., ETHYLENE) TO GIVE A MIXTURE OF OLEFINS (BOTH IN AN OUTSIDE OF PRODUCT RANGE) ALONG WITH LOWER ALKYL ORGANOMETALLIC. THIS MIXTURE IS CONVERTED TO A MIXED VAPORMIST SYSTEM WHERE OLEFINS HAVING MORE THAN ABOUT 16 CARBON ATOMS PER MOLECULE ARE IN THE MIST PHASE AND THE VOLATILE COMPONENTS ARE IN THE VAPOR PHASE AND THE VAPOR-MIST SYSTEM IS SEPARATED INTO TWO RESPECTIVE STREAMS IN AN INERTIA SEPARATOR. THE VAPOR PHASE COMPONENT STREAM IS THE FURNISHED AS FEED TO THE FIRST-NAMED REACTION SYSTEM.

May-16, 1972 c. w. LANIER PROCESS FOR THE PRODUCTION OF OLEFINS Filed Aug. 27', 1969 m0 PUDOOma OF United States Patent Office` 3,663,647 PROCESS FOR THE PRODUCTION OF OLEFINS Carroll W. Lanier, Baker, La., assignor to Ethyl Corporation, New York, N.Y. Filed Aug. 27, 1969, Ser. No. 853,306 Int. Cl. C07c 3/10 U.S. Cl. 260-683Jl D 27 Claims ABSTRACT 0F THE DISCLOSURE Olefins inthe range of 6-20 'carbon atoms are prepared by feeding lower olefin (e.g., ethylene), lower alkyl organometallic (e.g., triethyl aluminum) and product olefin into a reaction system in which chain build up occurs (e.g., chain growth or catalytic polymerization). The reaction efiiuent is flashed to remove product olefin and lower boiling olefin. The remainder of the effluent contains higher alkyl organometallic and is subjected to an alkyl displacement reaction using lower olefin (e.g., ethylene) to `give a mixture of olefins (both in and outside of product range) along with lower alkyl organometallic. This mixture is converted to a mixed vapormist system where olefins having more than about 16 carbon atoms per molecule are in the mist phase and the volatile components are in the vapor phase and the vapor-mist system is separated into two respective streams in an inertia separator. The vapor phase component stream is then furnished as feed to the first-named reaction system.

BACKGROUND OF THE INVENTION Field of the invention The invention relates to the preparation of higher molecular weight olefins predominantly of the vinyl type having unbranched carbon skeletal configuration and terminal unsaturation. In particular, the processing preferred involves a stepwise addition, growth or polymerization type of reaction employing lower olefin molecules such as ethylene as a building block using organometallic compounds or adjuvants such as triethyl aluminum as catalyst or as stoichiometrie reactant. In one aspect the invention relates to growth of ethylene on intermediate range olens such as decene-l without limitation as to source or prior history to produce higher olefins such as dodecene-l. In greater detail, the present invention relates to systems wherein olefin molecules of lesser molecular weight than the higher desired range and, optionally, adjuvants are circulated for growth reaction, The present improvement is directed more particularly to an improved processing step wherein the products of greater molecular weight than the higher desired range are separated from recycle streams economically without requiring fractional distillation thereby avoiding the progressive accumulation of heavies in the system and also avoiding investment and operating expenses attendant to fractional distillation in plate or packed towers operative with reflux.

Description of the prior art The foregoing separation is recognized to be particularly difficult in prior art processes because of overlapping boiling points of certain olefins and adjuvant materials, such as triethyl aluminum, generally co-present. The overlapping boiling points have long been an obstacle in the production of olens.

SUMMARY The present invention provides an olefin generation system which uses a stepwise adding, growing, or polymerizing reaction of olefin molecules in a reaction system in the presence of organometallic -growth adjuvant 3,663,647 Patented May 16, 1972 with separation and recycle of lower olefins and organometallic growth adjuvants. A particularly effective and low cost purge arrangement is provided for heavy olefins.

Separations of such a system are well known problem areas because certain valuable olefins, i.e., those having about l2 carbon atoms per molecule, have boiling points that correspond to that of the organometallic growth adjuvant usually most desired, viz, triethyl aluminum.

A problem of such a4 system is the difficulty of avoiding a gradual accumulation in the system of olefins of extremely high molecular weight such as those having above 18, or 20, or 22 or 24, or more, carbon atoms per molecule, depending upon the upper limit selected for the desired product olefin range.

The foregoing separations are so difiicult that in many instances valuable olefins and organo metal growth adjuvants are actually discarded together, rather than being separated and recovered, with attendant adverse effect upon the costs and prices for the materials that are recovered.

It is accordingly an object of the present invention to provide an olefin process wherein recovery of organometallic growth adjuvants such as organo aluminum compounds, and triethyl aluminum in particular, is facilitated to permit recycle of such materials and improved economics of the overall process.

Another object of the present invention is to provide a process wherein valuable olefins having from about l0 to about 16 carbon atoms per molecule are readily separated from organic aluminum growth adjuvants.

Another object of the present invention is to provide a process wherein the foregoing heavy olefins of extremely high molecular weight, such as those having about 18 and more carbon atoms per molecule, are readily separated at low cost from lower olefins and organic aluminum growth adjuvants whereby those heavy olefins are removed as useful materials and a build-up thereof in the recycle system is avoided.

Other and further objects and features of the present invention will become apparent upon careful consideration of the following discussion and the accompanying drawing, the single figure of which shows in block form a preferred embodiment of the features of the present invention.

DISCUSSION OF CLAIMED SUBJECT MATTER In accordance with the basic teachings of the present invention, a process is provided for producing oleus having from about 6 to about 20 or 30 carbon atoms per molecule particularly the more valuable ones having about 8-16 carbon atoms per molecule by processing including a stepwise adding, growing, or polymerizing reaction of lower olefin molecules in a reaction system in the presence of organometallic growth adjuvant. In particular, the present invention relates to an improvement in such processes.

One aspect of the improvement involves the flashing of olefin molecules of product range and lower molecular weight from the reaction effluent. Preferably excess lower olefin molecules are remoed by flashing as a preliminary aspects of this flashing yielding at least two different molecular weight categories of flashed olefins.

Another aspect of the improvement is that wherein at least a part of the product of the reaction remaining from the foregoing flashing is transalkylated with lower olefin molecules to produce a mixture containing olefin molecules and co-present organometallic growth adjuvant having organic constituency corresponding substantially to radicals formed from the olefin molecules used in transalkylation.

In the present process at least a part of said mixture from the foregoing transalkylation is converted to a mixed vapor-mist system in which the olefin molecules contained therein having more than about 16 carbon atoms per molecule are substantially all in the mist phase and substantially all higher vapor pressure molecules are in the vapor phase.

In addition to the foregoing, the process of the present invention involves the separation of the foregoing vapor phase and mist phase components of the vapor mists system into two respective streams by an inertia separator.

In certain preferred embodiments of the foregoing process, the inertia separator is a centrifugal vortex separator.

A further feature of the present invention is that at least a part of the vapor phase component stream from the foregoing vapor-mist separation is delivered to the reaction system.

In certain preferred embodiments of the present process, the stepwise reaction of growing or polymerizing is a chain growth addition or insertion reaction of ethylene, the organometallic growth adjuvant being trialkyl aluminum, the temperature being from about 200 F. to about 320 F. and the pressure being from about 100 atm. to about 250 atm.

In certain preferred embodiments of the process of the present invention, the transalkylation is a substitution or displacement or splitting-off and addition reaction with ethylene of at least part of the foregoing product of the reaction remaining after the flashing of olefins at a temperature from about 450 F. to about 600 F. and a pressure from about 3 atm. to about 30 atm. in the ratio of about 20 to about 100 mols of ethylene per mol of trialkyl aluminum and wherein substantially all trialkyl aluminum effluent from the transalkylation is triethyl aluminum.

In other preferred embodiments of the process of the present invention, the temperature in the separator is from about 400 F. to about 600 F. and the pressure is from about 3 atm. to about 30 atm.

In certain preferred embodiments of the process of the present invention, the vapor phase component from the separation that is delivered to the reaction system includes substantially the entire amount of product range olefin molecules derived in the transalkylation by conversion of higher alkyl-trialkyl aluminum compounds to triethyl aluminum and the said product range olefin molecules are carried through the reaction environment to be contained in the reaction eflluent.

In certain preferred embodiments of the process of the present invention, the vapor phase component stream delivered to the reaction system contains organometallic growth adjuvant for the reaction system.

In certain preferred embodiments of the process of the present invention, makeup organometallic growth adjuvant is fed to the reaction system in the form of trialkyl aluminum.

In certain preferred embodiments of the process of the present invention, the makeup trialkyl aluminum fed to the reaction system is triethyl aluminum.

In certain preferred embodiments of the process of the present invention, light olefin molecules ranging up to about decene-l are flashed from the mixture from the transalkylation prior to the conversion of part of said mixture to the vapor-mist system.

In certain preferred embodiments of the process of the present invention, at least a part of the olefin molecules lighter than product range are flashed from the reaction eflluent and are recycled to the reaction system.

In certain preferred embodiments of the process of the present invention, the product range olefins is from about dodecene-l to about heXadecene-l.

In certain preferred embodiments of the process of the present invention, at least a part of the light olefin molecules flashed from the mixture from the transalkylation are delivered to the reaction system.

In certain highly preferred embodiments of the process of the present invention, it is desired to produce olefins Cil having from about 8 to about 16 carbon atoms per molecule by a stepwise reaction in a reaction system using ethylene and organometallic growth adjuvant trialkyl aluminum at a temperature from about 245 F. to about 290 F. and a pressure of from about 133 atm. to about 200 atm. with makeup trialkyl aluminum fed to the system as triethyl aluminum. In greater particularity with regard to one aspect, the invention features are applied in such manner that at least part of the olefin molecules of product range and lighter molecular weight are flashed from the reactor eflluent after which at least a part of the remaining effluent of the reaction is transalkylated with ethylene at a temperature of from about 530 F. to about 575 F. and a pressure of from about 10 atm. to about 17 atm. and in a ratio of from 40 to about 80 mols of ethylene per mol of trialkyl aluminum to produce a mixture containing olefin molecules and co-present trlalkyl aluminum wherein substantially all trialkyl aluminum in the effluent from the transalkylation is triethyl aluminum and wherein at least a part of the effluent from the transalkylation is subjected to flashing whereby at least a part of the ethylene and other light olefin molecules ranging up to about hexene-l are removed therefrom.

In such certain highly preferred embodiments, materials remaining after the flashing just mentioned are converted to a mixed vapor-mist system at a temperature from about 400 F. to about 575 F. and a pressure of from about 10 atm. to about 17 atm. wherein the olefin molecules contained therein having more than about 16 carbon atoms per molecule are substantially all in the mist phase and substantially all higher vapor pressure molecules are in the vapor phase. Such vapor phase and mist phase components are separated into two respective streams by a centrifugal vortex separator. The vapor stream includes substantially the entire amount of product range olefin molecules derived in the transalkylation by conversion of higher alkyl-trialkyl aluminum compounds to triethyl aluminum and at least part of this stream is delivered to the reaction system for growth of the triethyl aluminum to higher alkyl aluminum compounds from which the C12 olefins are readily separated by flashing. In this system, product range olefin molecules in the stream just discussed are carried through the reaction system to constitute at least part of the olefin molecules flashed from the reaction effluent in the first recited step of the preceding paragraph. The part carried through is particularly that of about decene-l, dodecenel, and tetradecene-l since those lower and higher are separable from triethyl aluminum by distillation without great difficulty.

An additional aspect of certain preferred embodiments of the present process as set forth in the two preceding paragraphs is that at least a part of the light olefin molecules ranging up to about hexene-l flashed from the transalkylation effluent are delivered to the reaction system. This aspect is of particular significance in instances wherein it is desired to keep these olefins recirculating to ultimately achieve conversion thereof to molecules of product range molecular weight. In those instances where such light olefins can be used elsewhere or sold to advantage, such recycle is of lesser importance.

EXAMPLE OF APPARATUS AND FLOW With reference now to the drawing, the apparatus shown therein indicates a preferred combination of components and processing steps of a plant for producing higher olefins such as octene-l, decene-l, dodecene-l, tetradecene-l and eicosene-l from lower olefins such as ethylene, propylene, butylene, and the like, with peaking to selected molecular Weight product olefins. The apparatus of FIG. 1 contains a first component l0 which is illustrated as a chain growth operation wherein, for example, ethylene and a lower alkyl aluminum or boron or purpose equivalent alkyl metal compound, typically triethyl aluminum or diethyl aluminum hydride, are reacted to produce higher alkyl, alkyl aluminum compounds.

It is to be understood that in appropriate purity or cost instances the chain growth operation, which is preferred because of its recognized excellence in producing straight chain vinyl alpha yoleiins of high purity can be substituted or replaced entirely or in part by other unit operations such as catalytic polymerization or combined with other operations which produce part or all of the olefns delivered to the reaction system. Thus oleins may be obtained from alkanes by dehydrogenation, wax cracking, halogenation, dehydrohalogenation, oxidative dehydrogenation and the like. Typical catalysts for such catalytic polymerization or growth are trialkyl aluminum or boron compounds such as triethyl aluminum and organo and inorganic compounds of transition metals such as alkyls, alkoxides, hydrides or halides of titanium, zirconium, alkoxides or halides 'or various mixtures with or without copper, zinc, cadmium, tin, vanadium, antimony, lead bismuth, arsenic, phosphorus, and the like, such materials being used alone or in various combinations. Many examples of such catalysts and catalytic combinations are described in issued patents.

In any event, the effluent from the chain growth usually contains olens and/or organo metallic compounds in which the molecules contain organic radicals having from 2 to about 50 carbon atoms each which represent grown or polymerized or increased molecular weight organic materials.

As is common practice in olen processing operations involving stepwise addition, the higher alkyl orgauometallic compounds that are produced are subjected to a transalkylation or displacement reaction with one or more lower oleiins, typically ethylene, so as to produce lower alkyl oragnometallic compounds, typically then, triethyl aluminum, liberating higher oleiins corresponding in carbon skeletal structure to the alkyl radicals that were initially attached to the organometallic compounds obtained from the preceding (growth) operation. By using a high molecular ratio of molecules of lower olens (ethylene) to alkyl radicals in the feed, say 10:1 or higher; even 50:1 or 100:1, virtually complete conversion to lower alkyl structures (triethyl aluminum) is possible.

In this instance then, the chain growth operation 10 is followed by a transalkylation operation 11 with ethylene in a ratio from about 10:1 to 100:1 mols of ethylene per alkyl radical to convert the tri-higher-alkyl aluminum compounds into triethyl aluminum and thereby to release oletins corresponding in carbon skeletal configuration to the carbon skeletal conguration of the alkyl groups that had been attached to the alkyl aluminum compounds. In this way, one produces mixtures containing `oleiins ranging from ethylene up to oleiins having about iifty carbon atoms per molecule together with lower alkyl trialkyl aluminum material which predominates in ethyl compounds, particularly triethyl aluminum.

One of the familiar problems encountered in connection with the chain growth-ethylene displacement form of olefin generation system is the matter of separation of olelins and alkyls which is complicated by physical property characteristics such as an overlapping of boiling points of the olefins and aluminum alkyls engendered. To accomplish peaking, separation is necessary to recover products which have attained the desired molecular weight and, frequently, to permit recycle of those of lesser molecular weight for additional growth.

Unfortunately, one does not ordinarily obtain pure single alkyl aluminum trialkyl compounds such as trihexyl aluminum or trioctyl aluminum where one deals with growth processes. Generally, one obtains merely wide range statistical mixtures, particularly with polymerization which is worse in that respect than Ziegler chain growth. Except for certain peculiarities of non-normal alkyls and ethyl alkyls, the statistical relationships are carried even to individual molecules. This results in mixed compounds such as ethyl, hexyl, octyl-aluminum; dibutyl, octyl-aluminum; diethyl, butyl-aluminum; and so forth. The mixed alkyl nature of the aluminum organo compounds encountered in such systems provides composite boiling points making distillation separations into pure organo-aluminum compounds expensive at the present state of the art.

In addition to the foregoing, the slopes of the vapor pressure curves for most aluminum alkyl compounds are different from the slopes for olefins which means that as pressures change or vary, due to deliberate or fortuitous circumstances, even the overlapping relationships between the boiling points of the olelins and the aluminum alkyls change or shift. Thus, in some instances, one may observe a similarity of boiling points between triethyl aluminum and dodecene, while under somewhat dilferent conditions one may encouter similarities of boiling points between triethyl aluminum and decene or even octene.

Because of such complexities of separations and the substantial amount of separation effort that must be expended, the success or failure of an olefin production system usually must hinge upon economic considerations connected with the ability to find combinations of processing steps that enable some measure of success in making separations between olefius and aluminum alkyls between olefins of different molecular weights and between aluminum alkyls of different molecular weights. Such separations are difficult and economics is a powerful factor leading one to seek simple low cost effective separation systems.

It has been discovered that a centrifugal (gravity magnifying) separator can be used to advantage in a system such as the foregoing; however, as a practical matter, the use of centrifugal separators having mechanically moving parts is prohibitively expensive and cumbersome. Surprisingly, it has been discovered that a comparatively simple inertia separator or a cyclone or vortex type of centrifugal separtaor which does not require mechanically moving parts, when used in conjunction with temperaturepressure control to provide a mixed liquid-vapor stream, is a simple but elfective passive combination for performing some 0f the separations involved in systems of the foregoing type. In particular, it is useful in the separation of higher oleiins (C16 and higher) and higher aluminum alkyls from triethyl aluminum and oleiins up to about C14. Seemingly, the combination of tine liquid droplets of a thin, well-agitated mobile liquid film and of good Contact between liquid and vapor, provides efficient transfers and separations.

To this end, the combination of separator 12 and its associated pressure-temperature control typically is placed at some suitable point in a selective recycle line which connects the transalkylation stage 11 back to the growth stage 10. Typically, the separator 12 delivers in line 13, as recycle to the growth 10, triethyl aluminum plus oleiins having predominantly from about 6 to about 10 carbon atoms per molecule. Additionally, the separation 12 provides in line 14 trialkyl aluminum compounds having alkyl groups which aggregate more than 6 carbon atoms per 3 alkyl groups, together with higher olefins, particularly those having 16 and more carbon atoms per molecule.

Part or all of each of the foregoing streams of lines 13 and 14 can be sold or used in many instances without other separation and purification operations. In practice, it is frequently preferred to recover as much of the aluminum organic compounds as possible together with the lighter olefins and to recycle the light oleiins to additional chain growth or buildup through line 13 so as to produce olens in a selected molecular weight range. Typically then, part or all of either or both of the streams of lines 13 and 14 becomes subjected to distillation 15 wherein various oleiins fractions are produced, one typically being oleiins predominating in 12-16 carbon atoms per molecule in line 16, another being a stream predominating in triethyl aluminum and lighter oleiins in line 17.

The foregoing structure and operation of an elementary recycling system can be expanded and refined in numerous embodiments. One of the important aspects of the process is the control of conditions in and before the separation 12 so as to produce and maintain the mist-vapor stream delivered to the separation 12. The desired conditions are enhanced in one respect by attention to proportions or distributions by molecular weight with respect to the various components of the streams involved, their relative vapor pressures, and the like, and with careful attention to refinement by judicious choice of the points of withdrawal of various components of the complex streams.

What is frequently an important aspect of securing desired conditions in the separation 12 is a minimizing of the vapor volume burden imposed upon the separation by the lower molecular weight olefins, particularly those which are far removed in boiling point from those whose molecular weight is such that they are at a transition between a liquid phase and a vapor phase in the separation 12. Preferably this burden is handled easily and at low cost by several flash vaporization stages before and/or after the transalkylation 11.

Typically, the flash tandems 18 and 19 remove materials in several cuts such as recycle ethylene at lines 20 and 21. Typical second cuts removed at lines 22 and 23 are predominantly butene-l. Another typical stream is predominanntly hexene-l or hexene-l and octene-l at lines 24 and 25. Frequently, it is advantageous to remove at line 26 a cut of olefins ranging from about hexene through about tetradecene, a separation that is not too diicult at that point where the streams 22, 24 and 26 represent the flash from three sequential stages in that order and are virtually free of triethyl species of trialkyl aluminum.

The manipulations providing and utilizing the streams of lines 20-26 are capable of numerous variations. In the first place, in some instances it is desired to mix the ethylene streams of lines 20 and 21 with fresh ethylene feed for either or both of the transalkylation 11 or the chain growth 10. In many instances the ethylene recycle at 21 is local as shown to facilitate the use of high ratios such as 35:1 of mols of ethylene per alkyl radical in the environment of transalkylation 11 to enhance the substantially complete conversion of all other 'alkyl species to triethyl aluminum and to minimize adverse side reactions such as isomerization or dimerization of higher olefins. With high ratios one usually prefers to minimize heat exchanger loads by placing fiash tandem 19 after separation 12. In this instance the flash tandem is preceded by a partial condenser of at least the materials heavier than the ethylene, such ethylene being recycled to the transalkylation.

Although the light olefins streams of lines 22, 23, 24 and can be blended and fed to chain growth 10 for additional growth, it is evident that these streams can be withdrawn wholly or in part, individually or collectively, for use or sale with or without additional purification operations such as distillation. Frequently, it is desirable to remove for use or sale a butene-enriched streams such as the stream of lines 22 Iand 23 while returning only the predominantly hexene or octene streams of lines 24 and 25 to the chain growth 10.

One of the desired aspects of the operation of the ash tandems 18 and 19 is simplicity and low cost. It is of course evident that where one has unlimited funds and space available, one can obtain ve13I pure olefins using fractional distillation in tandems containing a plurality of multi-plate distillation columns; however, such a utopia is usually too expensive to be attractive for large scale commerci-al operations. Thus, a key to the operation of Athe whole system in addition to the judicious choice of conditions in the separation 12 is the selection and precise control of conditions in a plurality of Isimple charni'bers in fiash tandems 18 and 19. Thus, it is envisioned that the liash systems 18 and 19 include a plurality of chambers without any requirement for plates or packing 8 other than mist or entrainment elimination or separation and without the complication and expense of condenser and reflux systems usually associated with multi-plate or packed distillation towers.

The effectiveness of a simple inertia or cyclone separation 12 depends to a large extent upon the maintenance of proper temperature-pressure relationships in the system. A fundamental consideration for separation is the selection of physical conditions and co-presence materials that place one category of materials substantially entirely in the liquid phase in the cyclone separator and another category of materials substantially entirely in the vapor phase. Thus, unique effective combinations of agitation, gravity forces, centrifugal forces, boiling points and densities are brought into play and applied to enhance separation of a vapor-mist mixture or system cyclone separator 12 to yield separate etiiuent vapor and liquid (mist) phases.

The ancillary equipment involves generally one or more heat exchangers or, broadly, a temperature control device 27 appropriate to provide a desired heat content of the feed stream. The pressure in the separator system is maintained at a selected level by pressure controls 28, 29 which may be automatically or manually actuated. In simple versions, the controls 28 and 29 are mere throttling valves set to restrict effluent flow rates in the associated lines to maintain a selected pressure in cyclone 12. In more sophisticated systems, computer control coordinated with flow rates, and the like, are obvious extensions and desirable refinements.

In addition to the foregoing considerations, it generally is desirable to manipulate the temperature of the recycle stream of line 13 to optimize re-entry conditions for the chain growth 10. To this end, heat exchanger 30 is provided, for use when desired.

Inertia separators in their simplest form are represented by baffles or obstructions to flow in a pipe or chamber, the obstructions intercepting the mist without seriously impeding the fiow of vapor.

As the terms centrifugal separator or centrifugal vortex separator are used in connection with the present invention, it is intended to refer to simple static separators of the Itypes shown by Perry, Chilton and Kirkpatrick in Perrys Chemical Engineering Handbook, 4th ed., Mc- Graw-Hill Book Company (1963), pages 20-69. In utilizing such a system, the mixed vapor-mist system is supplied at a tangential inlet, or baflied in-line inlet, producing 'a circular motion within the separator which enhances the separation of the heavy mist. The vapor phase is removed at one outlet which normally is the upper or gas outlet in gas-solid separation systems. The mist phase is removed as a liquid at the bottom of the separator at the outlet which normally is that for the dust or solid material in a gas-solid separator. As a general proposition to maintain proper vapor phase flow and conditions within the separator, it is lpreferred that the lower outlet be provided with a liquid seal at the lower outlet to prevent unimpeded flow of the vapor through the lower outlet and to enhance stable flow conditions in the separator. The terms upper and lower are used in a descriptive sense rather than a limiting sense. In appropriate instances, the relationships between the terms and the streams may be reversed or otherwise altered.

It is evident, of course, that in many instances the centrifugal vortex separator is simply a cylindroconical outer vessel having merely a single inner cylindrical batiie but that various refinements with respect to complex baffling such as that also shown in the aforementioned reference at pages 26-69, can be useful and desirable.

In general, the centrifugal vortex type separator is well known to engineers, scientists and the public in general as thin sheet metal devices frequently associated with dust creating industrial processing such as rock crushers or saw mills and the like. Typically, sawdust is centrally collected from a plurality of wood cutting machines by a vacuum-pressure blower system and removed from discharge air by a vortex separator. It will be evident that vapor pressures of the present materials in many instances will require thicker walls in centrifugal vortex separators used in the present process than in those designed for use at substantially atmospheric pressure.

In an alternative embodiment the flash tandem 19 is placed in the main flow path between pressure control 28 and heat exchanger 30. The advantage of this in approximate instances is economy in the heat exchanger operations permitting 27 to be a minor cooling load.

In another embodiment, it is advantageous to purge a portion, say 1 to 5 percent by weight based on the aluminum content of the stream which goes from flash tandem 18 to transalkylation 11. The advantage of this modification is that it prevents the progressive build-up of certain materials in the system. In effect, this provides a desirable way to control the build-up within the system of materials of intermediate molecular weights, particularly the C14. In practice, this stream is usable for signicant value in numerous ways such as sale or conversion to other useful products such as alcohols, in which instance it is not a waste but is a useful operation. As a practical matter this purge stream is conveniently combined with the stream discharged from pressure control 29 and both delivered to such independent utilization as mentioned. In practice, the total quantity of purge at the two streams is virtually the entire aluminum loss of the system. The ratio of the two streams is variable up to zero quantity purge after 18 and more or less closely related in total quantity. A preferred ratio range is from about 3:1 to abount 1:3 with a typical ratio being about 1:2 by weight of the mist phase from the seperation 12 relative to the purge between 18 and 11.

Example I.-Apparatus was set up along the lines of the ligure, in an embodiment wherein a vent stream was taken after flash tandem 18 and flash tandem 19 was subsequent to the separation 12. The apparatus operated continuously with substantially the following conditions existing in the components. Principal flows are expressed in terms of pounds per hour.

Flow to chain growth include 291 pounds per hour of ethylene. This was equivalent to 154 fresh olefins plus 137 recycle from line 20; however, in this instance the recycle was collected and weighed and an equivalent extra quantity of fresh ethylene was fed to chain growth 10. Additional feed to 10 included 4.8 fresh triethyl aluminum and 532 recycle from 30 the latter stream containing 3.30 wt. percent aluminum mostly at TEA.

Approximately lbs/hr. of butene was withdrawn from the system rather than being recirculated. Hexene withdrawn amount to 28.1 lbs/hr. whereas octene and decene withdrawn amount to 91.8 lbs/hr. Materials heavier than decene withdrawn amounted to 50.9 lbs/hr. exclusive of the mist phase from 12. These materials analyzed about 95 percent by weight vinyl olens.

Flow to transalkylation 11 included 102 fresh ethylene plus about 847 recycle ethylene from the equivalent of line 21 but which, in this instance, is taken from a ash tandem after separator 12. Additionally, transalkylation 11 received about 463.8 of eluent from flash tandem 18, the actual effluent from 18 including an additional 18.2 lbs/hr. which was bled from the system as described in the foregoing. The effluent from 18 contained 3.64 wt. percent aluminum mostly in higher aluminum alkyl compounds.

In this example the separation 12 directly followed the transalkylation. Thus the approximately 1413 feed for transalkylation 11 was delivered to separation l2. The mist phase from separator 12 was 8.5 pounds per hour containing 0.6 wt. percent aluminum. This stream was collected and weighed without return to the system.

Example 11.-Apparatus was set up along the lines of the figure, in an embodiment wherein a vent stream was taken after flash tandem 18 and flash tandem 19 was subsequent to the separation 12. The apparatus operated continuously with substantially the following conditions existing in the components. Principal flows are expressed 1n terms of pounds per hour.

Tempera- Componont ture, F. Pressure Chain growth 10 268 2,700 p.s.i g. Tandem 18:

1st flash (C2) 110 85 p.s.i.g. 2d flash (C4) 285 0 p.s.i.g. 3d flash (Ca) 300 120 mm. Hg

absolute. 4th llash (Cs-10) 298 24 mm. Hg absolute. Transalkylation 11 560 220 psig. Separation 12 152 p.s.i.g. Distillation 15:

Bottom 285 Top 135 2d:

Bottom 436 Top 325 Flow to chain growth 10 included 301 pounds per hour of ethylene. This 'was equivalent to 104.4 fresh olelins plus 196.6 recycle from line 20; however, in this instance the recycle was collected and weighed and an equivalent extra quantity of fresh ethylene was fed to chain growth 10. Additional feed to 10 included 4.25 fresh triethyl aluminum and 445 recycle from 30, the latter stream containing 3.37 wt. percent aluminum mostly as TEA.

Approximately 20 lbs/hr. of butene was withdrawn from the system rather than being recirculated. Hexene withdrawn amounted to 9.49 lbs./hr. whereas octene and decene withdrawn amounted to 92.23 lbs/hr. Materials heavier than decene withdrawn amounted to 45.5 lbs./hr. exclusive of the mist phase from 12. These materials analyzed about percent by weight vinyl olefins.

Flow to transalkylation 11 included 94 fresh ethylene plus about 898 recycle ethylene from the equivalent of line 21 but which, in this instance, is taken from a flash tandem after separator 12. Additionally, transalkylation 11 received about 378.3 of eluent from flash tandem 18, the actual effluent from 18 including an additional 16.7 lbs/hr. which was bled from the system as described in the foregoing. The effluent from 18 contained 3.75 wt. percent aluminum mostly in higher aluminum alkyl compounds.

In this example the separation 12 directly followed the transalkylation. Thus the approximately 1370 feed for transalkylation 11 was delivered to separation 12. The mist phase from separator '12 was 4.14 pounds per hour containing 2.0 wt. percent aluminum. This stream was collected and weighed without return to the system.

I claim:

1. A process for producing olens in the range of about 6 to about 20 carbon atoms per molecule which comprises:

(a) feeding lower olefin and lower alkyl organometallic adjuvant and olefin falling in said range into a reaction system maintained under elevated tempera- 1 l ture and pressure reaction conditions to generate a reaction effluent including olefin molecules falling in said range, olefin molecules falling outside of said range and higher alkyl organometallic adjuvant;

(b) flashing from said effluent olefin below said range and product olefin within said range separable from the higher alkyl organometallic adjuvant;

(c) feeding lower olefin and at least part of the residue remaining after the flashing of (b) into a reaction system maintained under elevated temperature and pressure conditions to displace alkyl groups of the higher alkyl organometallic adjuvant and form a displacement mixture containing olefin molecules falling in said range, olefin molecules falling outside of said range and lower alkyl organometallic adjuvant;

(d) converting at least part of the displacement mixture to a mixed vapor-mist system in which the olefin molecules contained therein having more than about 16 carbon atoms per molecule are substantially all in the mist phase and substantially all higher vapor pressure molecules including lower alkyl organometallic adjuvant and olefin having up to about 16 carbon atoms per molecule are in the vapor phase;

(e) feeding the mixed vapor-mist system into an inertia separator to separate the vapor phase and mist phase components into two respective streams; and

(f) recovering from the inertia separator at least part of the vapor phase component stream thereby furnished as feed to (a) lower alkyl organometallic adjuvant and olefin falling in said range.

2. The process of claim 1 wherein in (e) the mixed vapor-mist system is fed into a centrifugal vortex separator.

3. The process of claim 1 wherein the lower alkyl organometallic adjuvant and the higher alkyl organometallic adjuvant are trialkyl aluminum compounds.

4. The process of claim 1 wherein the lower alkyl organometallic adjuvant and the higher alkyl organometallic adjuvant are trialkyl aluminum compounds and wherein the reaction of (a) is a chain growth reaction involving said lower olefin and trialkyl aluminum.

5. The process of claim 1 wherein the lower alkyl organometallic adjuvant and the higher alkyl organometallic adjuvant are trialkyl aluminum compounds and wherein the reaction of (a) is catalytic polymerization involving said lower olefin and t-rialkyl aluminum.

6. The process of claim 1 wherein the lower olefin fed in (a) and in (c) is ethylene.

7. The process of claim 1 wherein light olefin mole cules ranging up to about decene-l are fiashed from the displacement mixture prior to conversion of part of said mixture to the vapor-mist system.

8. The process of claim 1 wherein light olefin molecules ranging up to about decene-l are flashed from the displacement mixture prior to conversion of part of said mixture to the vapor-mist system and wherein at least some of these flashed light olefin molecules are delivered to the reaction system of (a).

9. The process of claim 1 wherein light olefin molecules ranging up to about decene-l are ashed from the displacement mixture prior to conversion of part of said mixture to the vapor-mist system, wherein at least some of these flashed light olefin molecules are delivered to the reaction system of (a), and wherein at least part of the olefin below said range ashed in (b) is delivered to the reaction system of (a).

10. A process for `producing product olefin within the range of about 6 to about 20 carbon atoms per molecule which comprises:

(a) reacting lower olefin with trialkyl aluminum in the presence of olefin falling in said range and under elevated temperature and pressure chain growth conditions to produce a higher molecular weight trialkyl aluminum chain growth product;

(b) flashing from the reaction efliuent of (a) product olefin and olefin falling below said range;

(c) reacting lower olefin with the trialkyl aluminum content of at least part of the residue remaining after the flashing of (b) and under elevated temperature and pressure alkyl displacement conditions to produce a displacement mixture containing olefin molecules falling in said range, olefin molecules falling outside of said range and co-present trialkyl aluminum having alkyl constituency corresponding substantially to alk'yl radicals formed from the olefin molecules used in the displacement reaction;

(d) converting at least a part of the displacement mixture to a mixed vapor-mist system in which the olefin molecules contained therein having more than 16 carbon atoms per molecule are substantially all in the mist phase and substantially all higher vapor pressure molecules including lower alkyl trialkyl aluminum and olefin having up to about 16 carbon atoms per molecule falling in said range are in the vapor phase;

(e) separating the vapor phase and mist phase components of the vapor-mist systems into two respective streams by means of an inertia separator; and

(f) delivering to (a) at least a part of the vapor phase component stream from the separation of (e) thereby furnishing to (a) lower alkyl trialkyl aluminum and olefin falling in said range.

11. The process of claim 10 wherein the separation of (e) is effected by means of a centrifugal vortex separator.

12. The process of claim 10 wherein said lower olefin in (a) and in (c) is ethylene.

13. The process of claim 10 wherein said lower olefin in (a) and in (c) is ethylene and wherein the chain growth reaciton of (a) is performed at a temperature of from about 200 F. to about 320 F. and a pressure of from about atmospheres to about 250 atmospheres.

14. The process of claim 10 wherein said lower olefin in (a) and in (c) is ethylene and wherein the displacement reaction of (c) is performed at a temperature of from about 450 F. to about 600 F. and a pressure of from about 3 atmospheres to about 30 atmospheres in a ratio of about 20 to about 100 mols of ethylene per mole of trialkyl aluminum whereby substantially all trialkyl aluminum effiuent from the displacement is triethyl aluminum.

15. The process of claim 10 wherein the temperature in said inertia separator is from about 400 F. to about 600 F. and the pressure in said inertia separator is from about 3 atmospheres to about 30 atmospheres.

16. The process of claim 10 wherein the vapor phase component stream from the separation of (e) that is delivered to (a) includes substantially the entire amount of product range olefin molecules derived in the displacement of product range olefin molecules derived in the displacement by conversion of higher alkyl trialkyl aluminum compounds to triethyl aluminum and wherein said product range olefin molecules are carried through the reaction of (a) and are contained in the reaction effluent therefrom.

17. The process of claim 10 wherein there is fed to (a), in addition to the lower alkyl trialkyl aluminum furinshed from (f), a make-up quantity of trialkyl alfiminum for chain growth.

18. The process of claim 10 wherein light olefin molecules ranging up to about decene-l are fiashed from the displacement mixture prior to conversion of part of said mixture to the vapor-mist system.

19. The process of claim 10 wherein light olen molecules ranging up to about dicene-l are flashed from the displacement mixture prior to conversion of part of said mixture to the vapor-mist system and wherein at least some of these fiashed light olefin molecules are delivered to the reaction system of (a).

20. The process of claim wherein at least part of the olefin below said range flashed in (b) is recycled to (a).

21. A process for producing olefins having from about 8 to about 16 carbon atoms per molecule which comprises:

(a) chain growing ethylene on trialkyl aluminum in the presence of olefin of product range and at a temperature of from about 200 F. to about 320 F. and a pressure of from about 100 atmospheres to about 250 atmospheres;

(b) fiashing from the reaction efiiuent of (a) olefin of product range and also olen of lower molecular weight;

(c) subjecting the trialkyl aluminum contained in at least part of the remainder of said reaction efiiuent to a displacement reaction with ethylene employing a temperature of from about 450 F. to about 600 F. and a pressure of from about 3 atmospheres to about 30 atmospheres and using a ratio of from about to about 100 mols of ethylene per mol of trialkyl aluminum to produce a mixture containing olefin molecules of product range, olefin molecules outside of the -product range and co-present trialkyl aluminum which is substantially entirely triethyl aluminum;

(d) converting at least a part of the effluent from the displacement reaction to a mixed vapor-mist system at a temperature of from about 400 F. to about 600 F. and a pressure of from about 3 atmospheres to about 30 atmospheres wherein the olefin molecules contained therein having more than about 16 carbon atoms per molecule are substantially all in the mist phase and substantially all higher vapor pressure molecules including triethyl aluminum and olefin of product range are in the vapor phase;

(e) separating said vapor phase and said mist phase components of the vapor-mist system into two respective streams by means of a centrifugal vortex separator in which the temperature is from about 400 F. to about 600 F. and the pressure is from about 3 atmospheres to about 30 atmospheres so that the separated vapor stream includes triethyl aluminum and substantially the entire amount of product range olefin molecules derived in the displacement reaction; and

(f) delivering to (a) at least a part of said separated vapor stream thereby furnishing triethyl aluminum for chain growth and olefin of product range, substantially all of said olefin being carried through the chain growth reaction system to constitute a portion of the olefins recovered by fiashing in (b).

22. The process of claim 21 wherein after the displacement reaction of (c) at least a part ofthe displacement reaction efliuent is subjected to flashing whereby light olefin molecules ranging up to about hexene-l are removed therefrom and wherein at least a part of the remainder of this reaction effiuent is converted per (d).

23. The process of claim 21 wherein make-up triethyl aluminum is fed to (a), wherein after effecting the separation of (e) the separated vapor stream is condensed at least in part and ethylene is removed therefrom and returned for use in the displacement reaction of (c), and wherein at least a part of the remaining separated vapor stream is delivered pursuant to (f).

24. The process of claim 21 wherein make-up triethyl aluminum is fed to (a), wherein at least a part of the olefin lighter than product range flashed in (b) is delivered t0 (a), wherein after the displacement reaction of (c) at least a part of the displacement reaction effluent is subjected to flashing whereby light olefin molecules ranging up to about hexane-1 are removed therefrom and delivered to (a) and at' least a part of the remainder of this reaction efliuent isconverted per (d), wherein after effecting the separation of (e) the separated vapor stream is condensed at least in part and ethylene is removed therefrom and returned for use in the displacement reaction of (c), and wherein at least a part of the remaining separated vapor stream is delivered pursuant to (f).

25. The process of claim 21 wherein the chain growth of (a) is performed at a temperature of from about 245 F. to about 290 F. and a pressure of from about 133 atmospheres -to about 200 atmospheres, wherein the displacement reaction of (c) is performed at a temperature of from about 530 F. to about 575 F. and a pressure of from about 10 atmospheres to about 17 atmospheres using a ratio of from about 40 to about mols of ethylene per mol of trialkyl aluminum, and wherein after the displacement reaction of (c) at least a part of the displacement reaction eiuent is subjected to fiashing whereby light olefin molecules ranging up to about hexene-l are, removed therefrom and delivered to (a) and at least a part of the remainder of this reaction efiiuent is converted per (d) at a temperature of from about 400 F. to about 575 F. and a pressure of from about 10 atmospheres to about 17 atmospheres.

26. A process for separating alen having above about 16 carbon atoms per molecule from a process stream additionally containing higher vapor pressure olefins and triethyl aluminum which comprises:

(a) converting said process stream to a mixed vapormist system in which the olefin molecules contained therein having more than about 16 carbon atoms per molecule are substantially all in the mist phase and substantially all of the triethyl aluminum and said higher Napor pressure olefins are in the vapor phase; and

(b) feeding the mixed vapor-mist system into an inertia separator wherein the temperature is from about 400 F. to about 600 F. and the pressure is from about 3 atmospheres lto about 30 atmospheres whereby said system is separated into two respective streams, the vapor stream containing said higher vapor pressure olefins and triethyl aluminum and the other stream containing said olefin having above about 16 carbon atoms per molecule.

27. The process of claim 26 wherein the conversion in (a) is performed at a temperature of from about 400 F. to about 575 F. and a pressure of from about 10 atmospheres to about 17 atmospheres.

References Cited UNITED STATES PATENTS 3,210,435 10/1965 Kennedy et a1. 26o-677 3,218,343 ll/1965 Acciarri et al. 260-448 3,227,773 1/ 1966 Roming 260683.15

fPAUL M. COUGHLAN, J R., [Primary Examiner U.S. Cl. X.R.

ggo UNITED lSTATES* PATENT OFFICE CERTIFICATE OF CORRECTIGN Patent No. v 5,665,6V7 Dated May 16, ll972 Inventor@ Carroll w. Lanier It is certified that error appears in the above-identified patent and that said Letters Patent are'hereby corrected as shown below:

V- i n Column .2, line 6C, reads "remoed", should read removed --5 lineY 6l, reads l "aspec ts YVshould reada-T aspect w Column 5, line 56, reads "oragnometallic", should read organometallic Column 6, line 58, reads "separtaor", should read separator Column 7, line 2T, reads "predominanntly", should read predominantly Column 8, line 69, reads "Q6-29", should read 526-569 Column 9, line 35, reads "abount", `should read about line 66, reads "at, should read as Column l2, line 55, reads "reaciton", should read reaction --5 lines 55 and 56, delete "of product range olefin molecules derived in the displacement "3 line 65, reads "furinshed", should read furnished line 7l, reads Hdicene-l", should read decenel Column lll, line 5C, reads "alefin", should read olefin signed and sealed this 20th day of March 1973.

(SEAL) Attest:

EDWARD M.FLETCHER,JR. ROBERT GOTTSCHALK Commissioner of Patents Attesting Officer 

